Method for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas

ABSTRACT

A method for the simultaneous removal of nitrogen oxides and laughing gas from a stream containing nitrogen oxides and laughing gas, wherein a first catalyst that contains cobalt and, as support, an inorganic metal oxide, and a second catalyst that contains iron and, as support, an inorganic metal oxide, are used. In particular the method is carried out in such a way that (a) the gas stream containing nitrogen oxides and laughing gas is reacted with a reducing gas, the reducing gas comprising a saturated hydrocarbon, in the presence of the first catalyst and (b) the gaseous product from step (a) is reacted with a reducing gas, the reducing gas comprising a saturated hydrocarbon, in presence of a second catalyst. The catalyst system can be used for the treatment of off-gases from a nitric acid plant.

CROSS REFERENCE TO RELATED APPLICATION

This is the 35 USC 371 national stage of international application PCT/NL02/00075 filed on Jan. 31, 2002, which designated the United States of America.

FIELD OF THE INVENTION

The invention relates to a method for the simultaneous removal of nitrogen oxides (NO_(x)) and laughing gas (N₂O) from a gas stream containing nitrogen oxides and laughing gas. In this description nitrogen oxides (NO_(x)) are understood to be NO, NO₂ and a mixture of NO and NO₂.

BACKGROUND OF THE INVENTION

Li and Armor [Appl. Catal. B3, 55–60, 1993] describe the Co-ZSM-5-catalysed simultaneous decomposition of NO and N₂O in the presence of methane or propane and oxygen: 2NO+CH₄+O₂→N₂+2H₂O+CO₂ 2N₂O→2N₂+O₂

It has been found that although NO is still converted with a high degree of conversion at low temperature, the degree of conversion of N₂O decreases sharply at lower temperature. A temperature in the range of 450° C. to 500° C. is found to be necessary for a high degree of conversion of N₂O (see Li and Armor: Table 1). Furthermore, it is found that the degree of conversion of NO is higher when pure oxygen is used instead of N₂O as oxygen source (see Li and Armor: Table 2). On the other hand, the reduction of N₂O proceeds less favourably when both methane and oxygen are present (see Li and Armor: Table 3). The highest degrees of conversion are achieved at 500° C.; at this temperature 97% of the N₂O and only 30% of the NO are converted. This method thus has the disadvantage that the temperature range in which acceptable conversion of both NO and N₂O takes place is relatively narrow. In addition, this temperature is relatively high (450–500° C.). Moreover, the supply of oxygen has an advantageous effect (higher degree of conversion of NO), but also an adverse effect (lower degree of conversion of N₂O).

Kögel et al. [Catal. Lett. 51, 23–25, 1998] describe the Fe-MFI-catalysed simultaneous decomposition of NO and N₂O in the presence of propane and oxygen. It has been found that although NO is still converted with a high degree of conversion at low temperature, the degree of conversion of N₂O decreases sharply at lower temperature (see Kögel et al.: FIG. 2): the maximum degree of conversion of NO (40%) is reached at 300° C. and at this temperature the degree of conversion of N₂O is only approximately 5%. Moreover, the undesired CO is formed as a by-product. However, this disadvantage can be eliminated if a Pt-promoted Fe-MFI is used (oxidation of CO to CO₂). However, this has an adverse effect on the degrees of conversion of NO and N₂O (see Kögel et al.: FIG. 3). A possible combination of this type of catalyst with the catalyst described by Li and Armor is not obvious because, inter alia, the optimum temperatures are very different (300° C. and 450–500° C., respectively).

Perez-Ramirez et al. [Appl. Catal. B, 25, 191–203, 2000] describe a dual-bed catalytic system intended for the removal of nitrogen oxides (NO and NO₂) from a gas stream. In the first step NO_(x) conversion takes place with the aid of a Pt/AC catalyst in the presence of propene as reducing agent. A major disadvantage of such a catalyst is that during the conversion of NO the formation of laughing gas takes place as the main reaction. Perez-Ramirez et al. therefore also studied whether this laughing gas formed can be effectively converted into nitrogen and oxygen in a second step in the presence of propene using Fe-ZSM-5. However, the use of these two catalysts has the disadvantage that two reactors have to be used because the optimum temperature ranges for the two catalysts are far apart (Pt/AC: optimum temperature is approximately 200° C.; Fe-ZSM-5: >430° C.; see also Perez-Ramirez et al.: FIG. 10). It is true that the required temperature for the Fe-ZSM-5 catalyst can be lowered to some extent by supplying additional propene to the second reactor (the product stream from the first reactor no longer contains any propene: see page 197, left-hand column, second paragraph; when propene is supplied to the reactor containing Fe-ZSM-5 a higher degree of conversion of N₂O is found; see page 199, right-hand column, second paragraph), but not to a sufficiently low value.

The reduction of N₂O with the aid of a saturated hydrocarbon and an Fe-zeolite catalyst is described in WO 99/49954. The preferred temperature at which this catalyst converts N₂O is below 350° C. It is neither described nor suggested that this catalyst can be used together with another catalyst for the simultaneous removal of nitrogen oxides (NO and NO₂) and N₂O.

The conversion of NO_(x) with the use of, inter alia, a Co-zeolite catalyst is described in U.S. Pat. No. 5,149,512. Here NO_(x) is understood to be a mixture of at least two nitrogen oxides, including laughing gas (see, for example, column 3, lines 55–59 and column 4, lines 44–48). However, the fact that in this patent NO_(x) is not used to refer to N₂O is confirmed by the later publication by Li and Armor in Appl. Catal. B 3, 1993, on page 56. The experiments show only conversions of NO and not conversions of N₂O. U.S. Pat. No. 5,149,512 thus does not explicitly describe whether such a catalyst is able to reduce laughing gas. The best degrees of conversion are obtained at 450° C. (see U.S. Pat. No. 5,149,512: Table 2). A combination of this cobalt catalyst for the conversion of NO with, for example, the abovementioned iron catalyst for the conversion of N₂O would, on the basis of the data described, give a catalyst combination with completely different operating temperatures for the different conversions (<350° C. and 450° C., respectively) and would probably give degrees of conversion for NO that are too low. Incidentally, on the basis of this patent (U.S. Pat. No. 5,149,512) it would be best to choose a rhodium catalyst for the conversion of NO (see U.S. Pat. No. 5,149,512: Tables 1, 2, 5, 8 and 9, from which it can be seen that in the presence of CH₄ and O₂ the rhodium catalyst yields a degree of conversion of 55%, compared with 26, 34, 27 and 34%, respectively).

A combination of an iridium catalyst and a platinum catalyst is described in U.S. Pat. No. 5,997,830.

In U.S. Pat. No. 5,524,432 a catalytic reduction of nitrogen oxide (this term includes laughing gas; see U.S. Pat. No. 5,524,432: column 5, lines 12–15) is described where a reducing agent that has to contain methane is used (see U.S. Pat. No. 5,524,432: Claim 1 and column 4, lines 47–56). The advantage of this method is said to be that ammonia is not required (see Example 11, lines 19–21). The catalytic reduction is followed by a catalytic oxidation of residual methane into carbon dioxide and water. The catalyst that is used for the catalytic reduction comprises a crystalline zeolite with an Si/Al ratio of 2.5 or more and the zeolite contains cobalt, nickel, iron, chromium and/or manganese cations (see column 4, lines 37–46). Co-ZSM-5 is explicitly described in Example 5. However, U.S. Pat. No. 5,524,432 does not teach the person skilled in the art that this catalyst is suitable for the reduction of laughing gas.

SUMMARY OR THE INVENTION

The aim of the present invention is to eliminate the disadvantages described above. The invention therefore relates to a method for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas, wherein a first catalyst that contains cobalt and, as support, an inorganic metal oxide, and a second catalyst that contains iron and, as support, an inorganic metal oxides are used.

It has been found that use of a specific sequence (1. cobalt-containing catalyst, 2. iron-containing catalyst) of the catalysts gives better results than, for example, a mixture of the two catalysts or a different sequence. The invention therefore also relates in particular to a method for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas, wherein:

-   -   (a) the gas stream containing nitrogen oxides and laughing gas         is reacted with a reducing gas, the reducing gas comprising a         saturated hydrocarbon, in the presence of a first catalyst that         contains cobalt and, as support, an inorganic metal oxide,     -   (b) the gaseous product from step (a) is reacted with a reducing         gas, the reducing gas comprising a saturated hydrocarbon, in the         presence of a second catalyst that contains iron and, as         support, an inorganic metal oxide.

Advantage of the present invention are that the simultaneous removal of nitrogen oxides and laughing gas can effectively take place over a broad temperature range. Another advantage of the present invention is that high degrees of conversion can be achieved at low temperatures, even in the case of high GHSV (gas hourly space velocities) values. Moreover, it is not necessary to supply additional reducing gas to step (b). Furthermore, the two steps (a) and (b) can be carried out in one, it not being necessary to heat or to cool the gas between steps (a) and (b). The use in step (a) of the catalyst that contains cobalt and, as support, an inorganic metal oxide has the advantage that no additional N₂O is produced.

The (first) catalyst used in step (a) is preferably the cobalt catalyst which is described in U.S. Pat. No. 5,149,512 and that is incorporated here by reference. That is to say this catalyst is preferably a crystalline zeolite having a silicon:aluminium ratio of 2.5 or above, the zeolite having been exchanged with an effective amount of a cobalt cation, preferably Co²⁺. In particular, the zeolite has been exchanged with 0.1 to 15% (m/m) cation, based on the total weight of the exchanged zeolite.

According to the invention, after exchanging with cobalt, the zeolite can then also be exchanged with approximately 0.01 to 2.0% (m/m) of an additional metal, based on the total weight of the exchanged zeolite, said additional metal being a metal of the third period of Groups 5 to 11 in the Periodic System of the Elements. The exchanged zeolite can furthermore be impregnated with 0.01 to 15% (m/m), in particular 0.1 to 8.0% (m/m), based on the total weight of the impregnated, exchanged zeolite, of anionic or neutral material that contains a metal from Group 5, 6, 7 or 11 of the Periodic System of the Elements.

The (second) catalysts used in step (b) are preferably those which are described in WO 99/49954 and NL A 1 012 983 and which are incorporated here by reference. That is to say this catalyst is preferably a crystalline zeolite having an SiO₂:Al₂O₃ ratio of less than 100, preferably less than 65 and in particular less than or equal to 40, the zeolite having been exchanged with an effective amount of an iron cation, preferably Fe²⁺. The zeolite is preferably at least partially exchanged with (NH₄)₂Fe(SO₄)₂.6H₂O. A preferred embodiment of the catalyst used in step (b) is Fe-ZSM-5. The catalyst used in step (b) can also be a promoted catalyst, the catalyst being promoted with one or more noble metals, the noble metal preferably being ruthenium, rhodium, palladium, gold or platinum. A palladium-promoted Fe-ZSM-5 catalyst is preferably used.

Preferred embodiments of the zeolite supports comprise the MOR and MFI types. The zeolites can be used in the sodium, potassium, ammonium or hydrogen form. The zeolite, the counter-ion and also the Si/Al ratio can be suitably chosen by those skilled in the art. This is described, inter alia, in standard works on zeolites and also in U.S. Pat. No. 5,149,512 and WO 99/49954 and a number of other cited documents.

According to the invention steps (a) and (b) are carried out in one reactor, the two catalysts being used in series in a stacked bed.

The reducing gas is preferably methane, propane, natural gas, n-butane or LPG (where LPG is a mixture containing propane and butane). The molar ratio of the added reducing agent with respect to the sum of the concentrations of laughing gas and nitrogen oxides is 0.1 to 100 and preferably 0.1 to 20.

The method according to the invention is preferably carried out at a temperature of 150° C. to 700° C. and in particular of 250° C. to 600° C. The pressure is preferably 1 to 50 bar absolute (bara) and in particular 1 to 15 bar absolute.

The invention also relates to a catalyst system for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas by means of a reducing gas, which catalyst system comprises the first and second catalysts as described above.

The catalyst system can be used for the treatment of off-gases from a nitric acid plant.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1: NO_(x) conversion by Catalyst I (Co-ZSM-5), Catalyst II (Fe-ZSM-5) and a serial combination of the two.

FIG. 2: N₂O conversion by Catalyst I (Co-ZSM-5), Catalyst II (Fe-ZSM-5) and a serial combination of the two.

FIG. 3: NO_(x) conversion by Catalyst I (Co-ZSM-5) and Catalyst III (Pd—Fe-ZSM-5) as a mixture and in serial combination.

FIG. 4: N₂O conversion by Catalyst I (Co-ZSM-5) and Catalyst III (Pd—Fe-ZSM-5) as a mixture and in serial combination.

FIG. 5: NO_(x) and N₂O conversion by a stacked bed catalyst of Catalyst IV (III(Co—Pd-MOR) and III (Pd—Fe-ZSM-5) using CH₄ as reducing gas.

EXAMPLES Catalysts Example 1

A zeolite exchanged with cobalt was prepared by exchanging 100 g Na-ZSM-5 (Alsi Penta SN 27, dried for 24 hours at 125° C.) with a solution of 29.2 g Co(NO₃)₂.6H₂O (Merck) in 3 litres of water for 24 hours at 80° C. The catalyst was then washed with water, dried and calcined for 5 hours at 550° C. The catalyst has a loading of 2.7% (m/m) cobalt.

Example 2

A zeolite exchanged with iron was prepared by adding 100 g NH₄-ZSM-5 powder (Alsi Penta SM 27, dried for 24 hours at 125° C.) to a solution of 38.9 g (NH₄)₂Fe(SO₄)₂.6H₂O (Merck) in 3 litres of water. Ion exchange then takes place for 24 hours at 80° C. After washing with water, the catalyst was dried for 16 hours at 80° C. and calcined for 5 hours at 550° C. The catalyst has a loading of 2.3% (m/m) iron.

Example 3

A promoted catalyst was prepared by impregnating 100 g of a catalyst according to Example 2 with 3.1 g of a solution of Pd(NO₃)₂ (10% (m/m) in nitric acid, Aldrich) in demineralised water so that the pores of the base material were precisely filled (so-called “incipient wetness impregnation”). The concentration of the noble metal precursor was adjusted such that a percentage by weight of Pd of 0.15 based on the total weight of the catalyst was obtained. Finally the catalyst was dried for 16 hours at 80° C. and calcined for 5 hours at 550° C. The catalyst had a loading of 2.7% (m/m) iron and 0.15% (m/m) palladium.

Test Apparatus

The reaction of NO, NO₂ and N₂O with propane was studied in an automated flow set-up. The gases N₂, air, NO, NO₂, N₂O and propane were introduced and the partial pressures (see Table 2) controlled by means of calibrated Mass Flow Controllers (Brooks). Water was added via a Liquiflow controller and a Controlled Evaporator Mixer (Bronkhorst). Analysis of the outflowing gases was carried out by means of a calibrated FTIR spectrophotometer (Elsag, Bailey, Hartmann & Braun, model MB 100). The catalysts were pressed to form a tablet, ground and sieved. The catalyst particles were in a stainless steel reactor. The gases were passed through a preheating section before they came into contact with the catalyst. The temperature was measured by means of thermocouples at the inlet and at the outlet of the catalyst bed. The temperature at the inlet of the catalyst bed is given in the test results. The pressure in the test set-up could be set to 1 to 5 bar absolute (bara). The carrier gas in the examples is N₂.

Example 4

In these experiments the degrees of conversion of NO, NO₂ and N₂O by a stacked bed of the following catalysts were determined: step (a) Co-ZSM-5 according to Example 1 (Catalyst I) and step (b) Fe-ZSM-5 according to Example 2 (Catalyst II).

The conditions are given in Table 1, the gas compositions in Table 2 and the degrees of conversion in Table 3.

TABLE 1 Volume 10 ml Flow 5 l/min GHSV 30000 l/h p 1 bara

TABLE 2 N₂O 1500 ppm H₂O 0.5% NO  500 ppm O₂ 2.5% NO₂   0 ppm C₃H₈ 1500 ppm

The starting material in all tests was the gas mixture in Table 2 (unless stated otherwise). Tests were also carried out using a mixture of NO and NO₂ instead of NO as the starting material. Comparable results were obtained in these tests.

TABLE 3 Cat. II I I + II Cat.bed 10 + 10 ml T 10 ml 10 ml NO_(x) (° C.) N₂O (%) NO_(x) (%) N₂O (%) NO_(x) (%) N₂O (%) (%) 280 18 46 0 3 39 58 309 66 47 0 15 86 62 338 90 39 1 44 98 72 368 98 30 9 88 100 94 399 100 23 59 99 100 100 431 100 17 85 99 100 98 462 100 13 96 95 100 94 491 100 11 99 88 100 88

The results in Table 3 are shown as a graph in FIGS. 1 and 2, from which it is clear that simultaneous efficient conversion of NO_(x) and N₂O is possible only with the catalyst combination.

Example 5

It should be possible to use the cobalt and iron catalysts as a mixture. A comparative example is given below in which the degrees of conversion of NO_(x) and N₂O in a reactor in which the catalysts are present as a mixture are compared with the degrees of conversion by the stacked bed catalyst system of the present invention. The conditions are given in Table 4 and the test results are shown in Table 5. The gas mixture from Table 2 and the Catalysts I (Co-ZSM-5 according to Example 1) and III (Pd—Fe-ZSM-5 according to Example 3) were used in the experiment.

TABLE 4 Volume 12.5 ml Flow 5 l/min GHSV 24000 l/h p 4 bara

TABLE 5 I 2.5 ml III  10 ml Configuration Mixture Stack T (° C.) N₂O (%) NO_(x) (%) N₂O (%) NO_(x) (%) 210 0 34 0 34 235 0 53 1 55 265 36 80 57 67 297 78 71 82 56 325 93 63 95 59 353 99 56 99 81 382 100 50 100 91 410 100 43 100 93 440 100 38 100 93 469 100 36 100 92 500 100 37 100 90

The test results from Table 5 are shown in FIGS. 3 and 4. It can be seen from these results that the N₂O conversion under these conditions is advantageous for the stack configuration, especially at lower temperatures. The NO_(x) conversion shows a substantial difference. Up to approximately 250° C. the degree of NO_(x) conversion for the mixture increases with increasing temperature; above this temperature the degree of NO_(x) conversion decreases. A complete conversion is thus impossible using a mixture of the Co and Fe catalysts. Surprisingly, the stack configuration under these conditions yields virtually complete conversion above approximately 380° C.

Example 6

In this example the various sequences of Catalysts I and II (see Example 4) were compared. The conditions are given in Table 6 and the results in Table 7. The gas composition was as in Example 4. It can clearly be seen from Table 7 that much better results are obtained with the sequence I–II, which can be seen in particular from the degree of NO_(x) conversion.

TABLE 6 Volume 0.3 ml Flow 0.15 l/min GHSV 30000 l/h p 1 bara

TABLE 7 I 0.15 ml II 0.15 ml II 0.15 ml I 0.15 ml T(° C.) N₂O (%) NO_(x) (%) N₂O (%) NO_(x) (%) 300 6 29 3 29 320 23 38 16 40 340 63 47 52 56 359 88 48 82 64 378 98 67 95 60 396 100 88 100 53 414 99 93 100 41 433 98 92 100 26 451 87 99 100 16 489 99 94 100 6

Example 7

In this example the effect of the addition of Catalyst III on the CO concentration was determined. Catalyst III is Catalyst II with 0.15% (m/m) Pd according to Example 3.

It can be seen that replacement of half of Catalyst II by Catalyst III leads to an appreciable reduction in the emission of CO (see Table 8 for the conditions and Table 9 for the results). The degree of NO_(x) and N₂O conversion is not adversely affected by the addition of Catalyst III. The gas composition was as in Example 4.

TABLE 8 Volume 20 ml Flow 5 l/min GHSV 15000 l/h p 1 bara

TABLE 9 Cat. I 10 ml I 10 ml II 5 ml II 10 ml III 5 ml Emission Conversion Emission Conversion T CO C₃H₈ N₂O NO_(x) CO C₃H₈ N₂O NO_(x) (° C.) (ppm) (ppm) (%) (%) (ppm) (ppm) (%) (%) 288 1588 561 39 58 111 494 48 54 316 1799 254 86 62 78 206 88 59 345 1816 159 98 72 61 106 99 73 375 1540 59 100 94 43 42 100 88 407 714 4 100 100 28 6 100 96 437 284 0 100 98 17 0 100 96 466 147 0 100 94 11 0 100 92 495 114 0 100 88 7 0 100 87

Example 8

In this example it is demonstrated that using the combination of Catalysts I and III high degrees of conversion of NO_(x) and N₂O are possible without the adverse formation of CO. It is also demonstrated in this example that high degrees of conversion of NO_(x) and N₂O are possible with a space velocity that is twice as high (30000 h⁻¹ instead of 15000 h⁻¹). The conditions and results are given in Tables 10 and 11, respectively. The gas composition was as in Example 4.

TABLE 10 Volume 10 ml Flow 5 l/min GHSV 30000 l/h p 4 bara

TABLE 11 I   5 ml I 5 ml II 2.5 ml III 5 ml Cat. III 2.5 ml T(° C.) N₂0 (%) NO_(x) (%) N₂0 (%) NO_(x) (%) 288 54 67 57 57 316 82 72 85 77 345 94 82 86 97 375 97 88 87 99 407 99 90 95 99 437 100 90 100 98 466 100 88 100 95 495 100 86 100 91

Example 9

In this example the effect of the pressure was determined. It is found that more NO_(x) and N₂O is converted at higher pressure. The effect for NO_(x) is most pronounced at low temperature. The CO emission is lower at higher pressure. The conditions are summarised in Table 12 and the results in Table 13. The gas composition was as in Example 4.

TABLE 12 I 10 ml  Volume 20 ml II 5 ml Flow 5 l/min III 5 ml GHSV 15000 l/h p 1 to 4 bara

TABLE 13 Pressure 1 bara 2 bara 4 bara CO NO_(x) CO N₂O NO_(x) CO N₂O T (° C.) (ppm) N₂O (%) (%) (ppm) (%) (%) (ppm) (%) NO_(x) (%) 288 111 48 54 69 72 68 22 81 82 316 78 88 59 23 95 67 13 98 89 345 61 99 73 17 100 78 10 100 97 375 43 100 88 12 100 90 8 100 99 407 28 100 96 7 100 96 7 100 99 437 17 100 96 4 100 96 5 100 98 466 11 100 92 4 100 94 4 100 96 495 7 100 87 4 100 90 3 100 93

Example 10

The reaction where for the Co catalyst a mordenite support was chosen instead of a ZSM-5 support (see Example 1), is described in this example. Methane was also selected instead of propane (see Table 2). For this reaction a Catalyst IV, Co-mordenite, was first prepared by impregnating 5 g MOR (mordenite from Zeolyst CBV 21A) with 1 g Co(NO₃)₂.6H₂O in solution (density 1.34 g/ml). The catalyst was promoted with a small amount of Pd (0.37% (m/m) Pd). The final Co concentration is 2.2% (m/m).

As described above, a reactor containing a stacked bed was used, the first catalyst in this example being the Co—Pd-MOR catalyst (Catalyst IV) and the second catalyst the Pd—Fe-ZSM-5 catalyst from Example 3 (Catalyst III). The conditions are given in Table 14. The gas composition is shown in Table 15.

TABLE 14 Volume   30 ml Flow   51/min GHSV 10000 l/h p   4 bara

TABLE 15 N₂O 1500 ppm H₂O 0.5% NO  500 ppm O₂ 2.5% NO₂   0 ppm CH₄ 2500 ppm

The test results are given in Table 16 and plotted as a graph in FIG. 5.

TABLE 16 IV 15 ml III 15 ml T (° C.) N₂O (%) NO_(x) (%) 290 20 1 317 27 8 345 45 33 374 71 76 404 91 97 433 96 96 463 92 100

It can be seen from these data that high degrees of conversion to virtually complete conversions can also be achieved with methane over a broad temperature range. 

1. Method for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas, wherein a first catalyst that contains cobalt and, as a support, a first inorganic metal oxide, and a second catalyst that contains iron and, as a second support, a second inorganic metal oxide, are used, and wherein each of the first and second inorganic metal oxide is a zeolite.
 2. Method according to claim 1, wherein: (a) the gas stream containing nitrogen oxides and laughing gas is reacted with a first reducing gas comprising a saturated hydrocarbon, in the presence of the first catalyst to obtain a gaseous product; and (b) the gaseous product from step (a) is reacted with a second reducing gas comprising a saturated hydrocarbon, in the presence of the second catalyst.
 3. Method according to claim 2, wherein steps (a) and (b) are carried out in one reactor.
 4. Method according to claim 3, wherein each of the first and second reducing gas is selected from the group consisting of propane, natural gas, n-butane or LPG.
 5. Method according to claim 1, wherein the support for the first catalyst is a crystalline zeolite having a silicon:aluminum ratio of 2.5 or above.
 6. Method according to claim 1, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than
 100. 7. Method according to claim 1, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than
 65. 8. Method according to claim 1, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than or equal to
 40. 9. Method according to claim 1, wherein the second catalyst comprises a promoted catalyst.
 10. Method according to claim 9, wherein the promoted catalyst has been promoted with Pt, Pd, Ru, Au or Rh.
 11. Catalyst system for the simultaneous removal of nitrogen oxides and laughing gas from a gas stream containing nitrogen oxides and laughing gas with a reducing gas, wherein the catalyst system contains a first catalyst that comprises cobalt and, as support, a first inorganic metal oxide, and contains a second catalyst that comprises iron and, as support, a second inorganic metal oxide, and wherein each of the first and second inorganic metal oxide is a zeolite.
 12. Catalyst system according to claim 11, wherein the catalysts are present in series in one reactor.
 13. Catalyst system according to claim 11, wherein the support for the first catalyst is a crystalline zeolite having a silicon:aluminum ratio of 2.5 or above.
 14. Catalyst system according to claim 13, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than
 100. 15. Catalyst system according to claim 13, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than
 65. 16. Catalyst system according to claim 13, wherein the support for the second catalyst is a crystalline zeolite having a SiO₂:Al₂O₃ ratio of less than or equal to
 40. 17. Catalyst system according to claim 13, wherein the second catalyst comprises a promoted catalyst.
 18. Catalyst system according to 17, wherein the promoted catalyst has been promoted with Pt, Pd, Ru, Au or Rh. 